[go: up one dir, main page]

WO1993003170A1 - Procede de fermentation pour la production de natamycine - Google Patents

Procede de fermentation pour la production de natamycine Download PDF

Info

Publication number
WO1993003170A1
WO1993003170A1 PCT/US1992/006323 US9206323W WO9303170A1 WO 1993003170 A1 WO1993003170 A1 WO 1993003170A1 US 9206323 W US9206323 W US 9206323W WO 9303170 A1 WO9303170 A1 WO 9303170A1
Authority
WO
WIPO (PCT)
Prior art keywords
natamycin
inoculum
fermentation
medium
yeast
Prior art date
Application number
PCT/US1992/006323
Other languages
English (en)
Inventor
Michael Allen Eisenschink
James R. Millis
Phillip Terry Olson
Original Assignee
Bio-Technical Resources
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Bio-Technical Resources filed Critical Bio-Technical Resources
Priority to EP92917836A priority Critical patent/EP0600983B1/fr
Priority to DE69209510T priority patent/DE69209510T2/de
Priority to CA002115038A priority patent/CA2115038C/fr
Publication of WO1993003170A1 publication Critical patent/WO1993003170A1/fr

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P19/00—Preparation of compounds containing saccharide radicals
    • C12P19/44—Preparation of O-glycosides, e.g. glucosides
    • C12P19/60—Preparation of O-glycosides, e.g. glucosides having an oxygen of the saccharide radical directly bound to a non-saccharide heterocyclic ring or a condensed ring system containing a non-saccharide heterocyclic ring, e.g. coumermycin, novobiocin
    • C12P19/62—Preparation of O-glycosides, e.g. glucosides having an oxygen of the saccharide radical directly bound to a non-saccharide heterocyclic ring or a condensed ring system containing a non-saccharide heterocyclic ring, e.g. coumermycin, novobiocin the hetero ring having eight or more ring members and only oxygen as ring hetero atoms, e.g. erythromycin, spiramycin, nystatin
    • C12P19/626—Natamycin; Pimaricin; Tennecetin

Definitions

  • the present invention relates to a process for producing natamycin characterized by inoculum preparation, inoculum propagation and fermentation.
  • Natamycin is a member of the polyene family of antimycotics.
  • the compound natamycin is a tetraene with a molecular weight of about 666, empirical formula corresponding generally to C 33 H47NO1 3 , and it contains a glycosidically-linked carbohydrate moiety, ycosamine.
  • Natamycin has an isoelectric point of about pH 6.5, and the structure exists typically in two configurations: the enol-structure and the keto- structure.
  • the present invention relates to fermentation by an organism capable of producing natamycin. Particularly the present invention is directed to preparing (e.g., ⁇ porulation) and propagating an inoculum comprising a Streptomyces species that, during fermentation, produces natamycin. The Streptomyces species is exposed to a series of predetermined environments and/or mediums which improve the rate at which natamycin is produced.
  • a suitable medium for inoculum propagation comprises: a) a protein nitrogen source in an amount of from about 2-16 g/1, normally about 8 g/1; and b) a metabolizable carbon source present in an amount which is sufficient to avoid total carbon depletion, usually 5-30 g/1 of medium, and normally about 15 g/1; 2.
  • a suitable medium used during fermentation to induce the inoculum to produce natamycin comprises: a) about 80-250 g/1 of a metabolizable carbon source; and b) a protein nitrogen source containing a high level of protein and trace ingredients.
  • the protein nitrogen source typically comprises a non-yeast protein nitrogen component and a yeast protein nitrogen component. These two protein nitrogen components are desirably present in a ratio ranging, respectively, from about 5:1 to 11:1 based on protein contents, and for best results about 8:1.
  • Usage of media possessing the above characteristics is a key aspect of the present invention which permits the Streptomyces species to produce natamycin in a cost-effective manner.
  • FIG. 1 is a schematic block diagram of the process which may be used in the invention for inoculum propagation.
  • Fig. 2 is a graphical representation of the three phases which occur during fermentation.
  • an organism capable of producing natamycin is placed into contact with a predetermined medium to produce an inoculum, and then into a predetermined fermentation production medium that will support maximum metabolic activity of the organism during further propagation and natamycin producing fermentation. During fermentation the organism enzymatically transforms at least a portion of the predetermined production medium into natamycin.
  • a preferred Streptomyces species comprises Streptomyces gilvosporeus which has been deposited previously with the American Type Culture Collection (ATCC) in Rockville, Maryland, United States of America, that is registered as ATCC No. 13326.
  • ATCC American Type Culture Collection
  • An inoculum is prepared from a spore suspension of the appropriate spores.
  • the inoculum of the appropriate Streptomyces species is subsequently fermented which produces high yields of natamycin when placed into the fermentation medium of the invention.
  • the inoculum is typically exposed to a series of propagation steps wherein each step increases the quantity of the natamycin producing Streptomyces cells. After the quantity of Streptomyces cells is adequate, the Streptomyces is exposed to an environment and/or a medium which is designed to enhance natamycin production when the Streptomyces species ferments.
  • the inoculum is started by collecting the spores of a natamycin producing Streptomyces species which was obtained from the American Type Culture
  • the spores are germinated to produce an actively growing culture of the Streptomyces species.
  • a sterilized e.g., autoclaved
  • agar slant is inoculated heavily with the actively growing culture of the Streptomyces species(e.g. , Streptomyces gilvosporeus or any other natamycin producing species) , and incubated until the slant is covered substantially entirely with spores.
  • the spores on the agar slant are scraped into a small amount of a liquid, such as water (e.g., distilled water), nutrient medium, etc. , to produce an aqueous spore suspension.
  • the resulting spore suspension is propagated to produce the inoculum for the fermentation operation (i.e., natamycin production).
  • the spore suspension used to begin inoculum propagation should contain a spore concentration of about 10 5 -10 10 CFU/ml, and, normally, at least about 10 8 CFU/ml.
  • a number of agar slant media can be used to promote sporulation of the culture of the Streptomyces species (e.g., S. gilvosporeus) , which will be used to form the spore suspension.
  • agar slant mediums typically comprise at least one member of the following group: yeast malt agar, Hickey-Turner agar, GYA agar, Pridha agar, potato dextrose, Bennett's agar, etc.
  • a high concentration (e.g., 10 8 CFU/ml), of viable spores within the spore suspension is a key aspect of the present invention.
  • concentration of spores is too low, it takes much longer to obtain, through inoculum propagation, the quantity of Streptomyces cells sufficient for cost- effective natamycin fermentation production.
  • a reduced quantity of spores within the suspension lengthens the total inoculum propagation time and increases the likelihood of a contamination(e.g. , by an unwanted organism) .
  • a low spore concentration within the suspension may tend to promote the formation of large, tightly packed mycelial pellets.
  • pellets are unsuitable for obtaining high yields of natamycin due to problems associated with oxygen transfer, mass transfer of nutrients into the pellets, etc. Should the size of mycelial pellets become undesirable, the pellets can be broken apart physically, such as by using a shear force (e.g. ,blending) .
  • aqueous spore suspension (e.g., _?. gilvosporeus) , discussed above, is germinated and cell multiplication continued until the number of organisms is adequate to be used as an aqueous inoculum for fermentation production of natamycin.
  • a suitable inoculum cell density comprises a dry cell weight of about 1-5 g/1 and is used at a volume of about 0.1-10% of the natamycin production medium volume.
  • the aqueous medium used for inoculum propagation determines the cell density and the metabolic state of the inoculum (e.g., an adequate density of healthy cells is desirable) .
  • a sufficient amount of protein nitrogen which contains complex growth factors (e.g., vitamins), inorganic elements (e.g. ,potassium,sodium,calcium,etc. ) , and trace elements(e.g., boron, cobalt, iron, copper, zinc, etc.), that are commonly present in the protein nitrogen source are needed to achieve an inoculum possessing the desired cell density and metabolic state.
  • the protein nitrogen source may be any source that will propagate the spore suspension into an inoculum that will produce the desired high yields of natamycin.
  • a metabolizable source of carbon must also be supplied to the aqueous inoculum medium in an amount which is sufficient to achieve the desired inoculum cell density.
  • the carbon source should not be depleted completely during the inoculum propagation. Depletion of the carbon source tends to alter adversely the metabolic state of the inoculum, which may lead to reduced yields of natamycin during fermentation.
  • a variety of aqueous inoculum media can be used effectively in accordance with the present invention, to obtain high yields of natamycin it is advantageous to use predetermined amounts of medium ingredients.
  • a suitable medium for inoculum propagation may be prepared in water (e.g., low mineral content water, distilled water, etc.), and comprises: a) a protein nitrogen source in an amount from about 2-16 g/1, normally about 8 g/1; and b) a metabolizable carbon source present in an amount which is sufficient to avoid total carbon depletion, usually 5-30 g/1 of medium, and normally about 15 g/1.
  • water e.g., low mineral content water, distilled water, etc.
  • a protein nitrogen source in an amount from about 2-16 g/1, normally about 8 g/1
  • a metabolizable carbon source present in an amount which is sufficient to avoid total carbon depletion, usually 5-30 g/1 of medium, and normally about 15 g/1.
  • Composition 1 Difco "Bacto" peptone
  • composition 2 Hormel peptone PSR 5
  • the inoculum medium which provides nutrients that enhances the production rate of Streptomyces cells may be prepared by conventional techniques(e.g. , separate or simultaneous sterilization of the carbon and nitrogen sources at temperatures of about 120-140°C) .
  • the inoculum medium after sterilization desirably has a pH of about 7.
  • the spore suspension is introduced to the inoculum medium and the inoculum medium is heated to a temperature of about 25 - 40°C and, normally, about
  • the inoculum propagation may be conducted in a manner which achieves an exponential increase in the quantity of cells.
  • it is advantageous to keep the culture in an exponential growth mode during propagation by effectively increasing the volume of the inoculum during each step of the propagation. This can be done by either minimizing the duration of each step or by minimizing the number of steps. For example, once a predetermined cell density of inoculum has been achieved, the inoculum is transferred to a larger environment(e.g. , vessel), for further propagation.
  • an individual step in the series of inoculum propagation steps is permitted to continue depends upon the composition of the medium, quantity of Streptomyces cells desired, temperature, etc. Typically, an individual propagation step is conducted for about 6 through about at least about 24 hours.
  • the inoculum propagation process requires aeration of the inoculum.
  • the vessel or flask housing the inoculum may be agitated on a rotary shaker at about 200 rpm.
  • the inoculum may be agitated by an impeller which is located within the vessel that houses the inoculum while sterile air is forced into the bottom of the vessel.
  • Figure 1 is a schematic of the process which may be used to produce the inoculum that is fermented to produce nataymcin.
  • Figure 1 illustrates the volumetric increases in the inoculum which are achieved by propagation that are necessary to obtain a quantity of inoculum that is adequate to produce natamycin in a cost-effective manner.
  • the volume of inoculum is increased from 25 liters to 1250 liters by adding the 25 liters of inoculum to a vessel containing 1225 liters of an aqueous inoculum medium.
  • Natamycin production is conducted in a fermentation vessel which is capable of housing the fermentation process.
  • One element important for achieving maximum yields of natamycin is the composition of the aqueous fermentation medium.
  • the fermentation medium must contain the proper amounts of metabolizable carbon and protein nitrogen.
  • the medium contains complex growth factors (e.g. , vitamins) , and inorganic elements (e.g., potassium, sodium, calcium, etc.), and trace elements (e.g., boron, cobalt, iron, copper, zinc, etc.), that are commonly present in the protein nitrogen source.
  • a suitable medium for fermentation may be prepared in water(e.g., low mineral content tap water, distilled water, etc.), and comprises: a) about 80-250 g/1 of a metabolizable carbon source; and b) at least 15 g/1 and, normally about 20 g/1 through 80 g/1, of a protein nitrogen source containing a high level of protein and trace ingredients.
  • the protein nitrogen source may comprise a non-yeast protein nitrogen component and a yeast protein nitrogen component. These two protein nitrogen components are usually present in the ratio ranging, respectively, from about 5:1 to 11:1 based on protein contents, and for best results generally about 8:1.
  • the protein nitrogen source may be supplied from a wide range of sources.
  • soy protein products e.g. , isolates, flours, meals, etc.
  • the protein nitrogen may also comprise beef extract, protein ydrolysates (e.g. ,peptones) , and/or yeast (e.g., extracts, autolysates, etc.).
  • the production medium must also include a source of carbon which is metabolizable by the Streptomyces species.
  • the carbon source may supplied in any expedient form such as glucose, polysaccharide, corn and potato starches, etc.
  • the carbon source which is required to produce natamycin is not adequate for complete fermentation
  • carbon source addition may be performed during the natamycin production so as to maintain a quantity of carbon source of about 5-30 g/1, and usually 20 g/1.
  • an appropriate quantity of a suitable carbon source is added to the fermentation medium either initially and/or added after the fermentation has begun.
  • the carbon source may be present in the fermentation medium in an amount of about 40-100 g/1.
  • carbon source is continually added to the fermentor at a rate which is at least equivalent to the rate at which the carbon source is consumed by the Streptomyces species during the fermentation process(e.g. , to maintain the carbon source concentration at or above a minimum level) .
  • the carbon source addition is discontinued so that little or no carbon source is left at the end of the fermentation cycle (e.g., the quantity of the carbon source substantially equates to the particular quantity of carbon source within the fermentation medium which is necessary to complete the fermentation process) .
  • the natamycin production medium which provides nutrients for the Streptomyces fermentation and natamycin production is prepared by conventional techniques (e.g., separate or simultaneous sterilization of the carbon and nitrogen sources at temperatures of about 120-140°C) .
  • the production medium after sterilization, desirably has a pH of about 7.
  • the inoculum is introduced into a fermentation vessel until a concentration of about to 0.1-10%, usually about 2%, by volume is achieved in the production medium(e.g., the quantity of inoculum may be sufficient to inoculate a plurality of fermentors) .
  • the remainder of the volume of the fermentor comprises the fermentation medium.
  • Any technique is acceptable for introducing the inoculum to the production medium within the fermentor which delivers the inoculum in an active metabolic state.
  • the fermentation or production medium is brought to a temperature of about 25°-40°C, and normally 28°-35°C.
  • the length of time which the fermentation process is allowed to continue depends upon the composition of the fermentation medium, te perature, quantity of Streptomyces cells in the inoculum, quantity of natamycin desired, etc.
  • the fermentation process is conducted for about 70 through at least about 168 hours.
  • Oxygen is supplied to the natamycin production medium during fermentation. It is advantageous to maintain a dissolved oxygen level in the production medium of about 20%-80% of air saturation during the major portion of the fermentation. The ability to achieve a suitable dissolved oxygen level may be enhanced by proper coordination of the aeration and/or agitation rate.
  • the fermentation or production medium is aerated by forcing air(e.g., sterile air), through the fermentation medium, usually at a rate of about 0.3 through at least about 1.0 volumes of air per volume of fermentation medium.
  • air e.g., sterile air
  • the first phase includes addition of the carbon source to the fermentation medium and growth or multiplication of the Streptomyces species.
  • the first phase is also accompanied by natamycin production.
  • the concentration of natamycin in the fermentation broth increases as the progagation of the cells of the Streptomyces species increases.
  • the increase in the concentration of natamycin increases generally exponentially with time during the first phase.
  • the concentration of natamycin will increase constantly with time, which indicates that the second phase (i.e., the major phase) of natamycin production as been achieved.
  • the third phase is characterized by a plateau in the concentration of natamycin (e.g., which may be due to a slowing of the metabolic activities of the Streptomyces species) .
  • concentration of natamycin within the fermenter may be analyzed with respect to time in order to ascertain the current phase of fermentation. It is desirable to use a medium and/or an environment which induces the second phase of fermentation to be rapidly reached and maintained in order to maximize the overall quantity of natamycin that is produced.
  • an anti-foaming agent e.g. a silicone de-foamer
  • it may be desirable to add an anti-foaming agent e.g. a silicone de-foamer
  • an anti-foaming agent e.g. a silicone de-foamer
  • the natamycin production medium after inoculum addition has a pH of about 7.0, which decreases slowly during fermentation to about 4.5.
  • the lowered pH is a result of the metabolic activities of the Streptomyces species.
  • the resultant fermentation broth will normally include at least about 5 g/1 of natamycin.
  • the level of natamycin production may range from about 7 g/1 through at least about 12 g/1.
  • the natamycin can be separated from the production medium. In certain cases, the natamycin may be extracted from the fermentation broth and crystallized. Examples of acceptable techniques for obtaining crystalline natamycin can be found in U.K. Patent No. 846,933.
  • agar slants of the following compositions are prepared using distilled .water.
  • An inoculum medium of the following composition was prepared in distilled water, and the pH was adjusted to about 7.0 with potassium hydroxide. 20 g/1 glucose
  • Streptomyces gilvosporeus American Type Culture Collection Registration No. 13326, was obtained from the American Type Culture Collection as a freeze-dried spore suspension and used as the culture source. The culture was held on the agar slants at about 25°C until the culture sporulated.
  • the agar slants sporulated heavily within about 10 days and were used after 10-20 days. Spores were scraped off these agar slants into the inoculum medium to achieve a spore suspension concentration of about 10 8 CFU/ml. About 2 ml of the spore suspension was added to about 100 ml of the inoculum medium in a 500 ml baffled flask. The inoculum in the baffled flask was incubated for about 48 hours at about 29°C and agitated at about 200 rpm on a rotary shaker.
  • the natamycin production medium used in this Example was of the following initial composition:
  • the production medium was heated to about 29°C and the glucose was added to achieve an initial concentration of glucose of about 40 g/1.
  • the inoculum discussed above containing Streptomyces gilvosporeus was added to the fermentation vessel until the fermentation vessel had an inoculum content of about 2% by volume.
  • Glucose was added to the inoculum after about 40 hours of fermentation in order to maintain a glucose concentration of about 20 g/1 glucose in the fermentation vessel. This was done by feeding glucose to the fermenting vessel at a rate of about 1 g/l-hr. The agitation rate of the fermentation vessel was increased as necessary to maintain a dissolved oxygen level of about 50% of air saturation.
  • Test #1 The procedure of Test #1 was repeated with the following exception: a sparsely sporulated agar slant was used to prepare the spore suspension and, as a result, the spore concentration in the initial spore suspension was only about 5xl0 4 CFU/ml. The yield of natamycin was reduced to about 5.2 g/1 in 8.7 1 of fermentation broth (45 g natamycin total).
  • Test #1 The procedure of Test #1 was repeated with the following exception: the fermentation medium was changed to about 10 g/1 glucose, about 2 g/1 beef extract, about 2 g/1 yeast extract, about 0.5 g/1 asparagine and about 0.5 g/1 dibasic potassium phosphate. No glucose was added subsequently. After about 72 hours of production, the yield of natamycin was about 0.75 g/1 in about 0.1 1 of fermentation broth.
  • Tests 1 through 4 in this Example illustrates that an increase in the concentration of the spores in the inoculum and the nutrient content within the fermentation medium tends to increase the overall quantity of natamycin which may be recovered.

Landscapes

  • Organic Chemistry (AREA)
  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Zoology (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Microbiology (AREA)
  • General Chemical & Material Sciences (AREA)
  • Biotechnology (AREA)
  • Health & Medical Sciences (AREA)
  • Biochemistry (AREA)
  • Bioinformatics & Cheminformatics (AREA)
  • General Engineering & Computer Science (AREA)
  • General Health & Medical Sciences (AREA)
  • Genetics & Genomics (AREA)
  • Preparation Of Compounds By Using Micro-Organisms (AREA)
  • Micro-Organisms Or Cultivation Processes Thereof (AREA)

Abstract

L'invention concerne un procédé de fermentation d'une espèce de Streptomyces afin de produire de la natamicyne. Une suspension de spores de l'espèce de Streptomyces se propage dans un milieu prédéterminé afin d'obtenir une quantité de cellules de Streptomyces. Les cellules de Streptomyces fermentent dans un milieu de production prédéterminé afin de produire une quantité récupérable de natamycine.
PCT/US1992/006323 1991-08-05 1992-08-05 Procede de fermentation pour la production de natamycine WO1993003170A1 (fr)

Priority Applications (3)

Application Number Priority Date Filing Date Title
EP92917836A EP0600983B1 (fr) 1991-08-05 1992-08-05 Procede de fermentation pour la production de natamycine
DE69209510T DE69209510T2 (de) 1991-08-05 1992-08-05 Fermentationsprozess zur herstellung von natamycin
CA002115038A CA2115038C (fr) 1991-08-05 1992-08-05 Procede de fermentation pour la production de natamycine

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US74054591A 1991-08-05 1991-08-05
US740,545 1991-08-05

Publications (1)

Publication Number Publication Date
WO1993003170A1 true WO1993003170A1 (fr) 1993-02-18

Family

ID=24976976

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US1992/006323 WO1993003170A1 (fr) 1991-08-05 1992-08-05 Procede de fermentation pour la production de natamycine

Country Status (11)

Country Link
EP (1) EP0600983B1 (fr)
CN (1) CN1043659C (fr)
AU (1) AU2427992A (fr)
CA (1) CA2115038C (fr)
DE (1) DE69209510T2 (fr)
ES (1) ES2085031T3 (fr)
IL (1) IL102731A (fr)
MX (1) MX9204546A (fr)
NZ (1) NZ243848A (fr)
WO (1) WO1993003170A1 (fr)
ZA (1) ZA925876B (fr)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5591438A (en) * 1990-12-07 1997-01-07 Bio-Technical Resources L.P. Natamycin recovery
WO2007039572A1 (fr) * 2005-10-04 2007-04-12 Dsm Ip Assets B.V. Préparation antifongique améliorée
CN115323020A (zh) * 2022-07-21 2022-11-11 河北圣雪大成制药有限责任公司 一种用于生产纳他霉素的发酵培养基
CN115505615A (zh) * 2022-11-09 2022-12-23 淮北师范大学 一种基于链霉菌混菌发酵合成纳他霉素的方法
CN119776231A (zh) * 2025-01-23 2025-04-08 淮北师范大学 一种褐黄孢链霉菌zy8及其发酵种子和应用

Families Citing this family (21)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101062934B (zh) * 2007-05-31 2010-05-19 山东鲁抗医药股份有限公司 从发酵技术培养物中提取纳他霉素的方法
AU2009281457A1 (en) 2008-08-14 2010-02-18 Bayer Cropscience Ag Insecticidal 4-phenyl-1H-pyrazoles
EP2204094A1 (fr) 2008-12-29 2010-07-07 Bayer CropScience AG Procédé pour l'utilisation améliorée d'un potentiel de production d'introduction de plantes transgéniques
EP2227951A1 (fr) 2009-01-23 2010-09-15 Bayer CropScience AG Utilisation des composés d'énaminocarbonyle de combattre des virus transmis par les insectes
EP2555619A2 (fr) 2010-04-06 2013-02-13 Bayer Intellectual Property GmbH Utilisation de l'acide 4-phényl butyrique et/ou de ses sels pour augmenter la tolérance au stress chez des végétaux
BR112012025848A2 (pt) 2010-04-09 2015-09-08 Bayer Ip Gmbh uso de derivados do ácido (1-cianociclopropil) fenilfosfínico, os ésteres do mesmo e/ou os sais do mesmo para aumentar a tolerância de plantas a estresse abiótico.
UA110703C2 (uk) 2010-06-03 2016-02-10 Байєр Кропсайнс Аг Фунгіцидні похідні n-[(тризаміщений силіл)метил]-карбоксаміду
KR20130088022A (ko) 2010-06-03 2013-08-07 바이엘 크롭사이언스 아게 Ｎ-[(헤트)아릴알킬] 피라졸 (티오)카르복사미드 및 이의 헤테로치환된 유사체
EP2474542A1 (fr) 2010-12-29 2012-07-11 Bayer CropScience AG Dérivés fongicides d'hydroximoyl-tétrazole
AR085585A1 (es) 2011-04-15 2013-10-09 Bayer Cropscience Ag Vinil- y alquinilciclohexanoles sustituidos como principios activos contra estres abiotico de plantas
AR090010A1 (es) 2011-04-15 2014-10-15 Bayer Cropscience Ag 5-(ciclohex-2-en-1-il)-penta-2,4-dienos y 5-(ciclohex-2-en-1-il)-pent-2-en-4-inos sustituidos como principios activos contra el estres abiotico de las plantas, usos y metodos de tratamiento
US20140173770A1 (en) 2011-06-06 2014-06-19 Bayer Cropscience Nv Methods and means to modify a plant genome at a preselected site
BR112014000267A2 (pt) 2011-07-04 2016-09-20 Bayer Ip Gmbh utilização de isoquinolinonas, isoquinolinedionas, isoquinolinetrionas e dihidroisoquinolinonas substituídas ou, em cada caso, sais das mesmas como agentes ativos contra o stress abiótico em plantas
WO2013020985A1 (fr) 2011-08-10 2013-02-14 Bayer Intellectual Property Gmbh Combinaisons de composés actifs comprenant des dérivés spécifiques d'acide tétramique
WO2013023992A1 (fr) 2011-08-12 2013-02-21 Bayer Cropscience Nv Expression spécifique des cellules de garde de transgènes dans le coton
US20140378306A1 (en) 2011-09-16 2014-12-25 Bayer Intellectual Property Gmbh Use of 5-phenyl- or 5-benzyl-2 isoxazoline-3 carboxylates for improving plant yield
PH12014500564A1 (en) 2011-09-16 2022-05-02 Bayer Ip Gmbh Use of phenylpyrazolin-3-carboxylates for improving plant yield
PH12014500562A1 (en) 2011-09-16 2014-04-14 Bayer Ip Gmbh Use of acylsulfonamides for improving plant yield
EP2757886A1 (fr) 2011-09-23 2014-07-30 Bayer Intellectual Property GmbH Utilisation de dérivés d'acide 1-phényl-pyrazol-3-carboxylique à substitution en position 4 en tant qu'agents actifs contre le stress abiotique chez les végétaux
US9408386B2 (en) 2012-02-22 2016-08-09 Bayer Intellectual Property Gmbh Use of succinate dehydrogenase inhibitors (SDHIs) for controlling wood diseases in grape
CN104611283B (zh) * 2012-12-27 2018-09-21 北京市农林科学院 一种重组利迪链霉菌及其应用

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB846933A (en) * 1956-07-23 1960-09-07 American Cyanamid Co New antifungal substance, pimaricin, and method of producing same
CH359517A (de) * 1956-03-13 1962-01-15 Koninklijke Gist Spiritus Verfahren zur Herstellung von Pimaricin

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CH359517A (de) * 1956-03-13 1962-01-15 Koninklijke Gist Spiritus Verfahren zur Herstellung von Pimaricin
GB846933A (en) * 1956-07-23 1960-09-07 American Cyanamid Co New antifungal substance, pimaricin, and method of producing same

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5591438A (en) * 1990-12-07 1997-01-07 Bio-Technical Resources L.P. Natamycin recovery
WO2007039572A1 (fr) * 2005-10-04 2007-04-12 Dsm Ip Assets B.V. Préparation antifongique améliorée
EP2260706A2 (fr) 2005-10-04 2010-12-15 DSM IP Assets B.V. Composition anti-fungicide ameliorée
EP2260706A3 (fr) * 2005-10-04 2011-05-04 DSM IP Assets B.V. Composition anti-fungicide ameliorée
US8187844B2 (en) 2005-10-04 2012-05-29 Dsm Ip Assets B.V. Anti-fungal composition
US8536144B2 (en) 2005-10-04 2013-09-17 Dsm Ip Assets B.V. Anti-fungal composition
CN115323020A (zh) * 2022-07-21 2022-11-11 河北圣雪大成制药有限责任公司 一种用于生产纳他霉素的发酵培养基
CN115505615A (zh) * 2022-11-09 2022-12-23 淮北师范大学 一种基于链霉菌混菌发酵合成纳他霉素的方法
CN119776231A (zh) * 2025-01-23 2025-04-08 淮北师范大学 一种褐黄孢链霉菌zy8及其发酵种子和应用

Also Published As

Publication number Publication date
IL102731A (en) 1996-01-31
IL102731A0 (en) 1993-01-31
CN1043659C (zh) 1999-06-16
ZA925876B (en) 1994-02-07
DE69209510D1 (de) 1996-05-02
EP0600983A1 (fr) 1994-06-15
CA2115038C (fr) 2002-10-22
ES2085031T3 (es) 1996-05-16
MX9204546A (es) 1993-02-01
EP0600983B1 (fr) 1996-03-27
NZ243848A (en) 1995-07-26
CN1071460A (zh) 1993-04-28
DE69209510T2 (de) 1996-10-10
CA2115038A1 (fr) 1993-02-18
AU2427992A (en) 1993-03-02

Similar Documents

Publication Publication Date Title
EP0600983B1 (fr) Procede de fermentation pour la production de natamycine
US5231014A (en) Fermentation process for producing natamycin
El‐Enshasy et al. Influence of inoculum type and cultivation conditions on natamycin production by Streptomyces natalensis
US5686273A (en) Fermentation process for producing natamycin with additional carbon and nitrogen
US4400467A (en) Process of using xanthomonas campestris NRRL B-12075 and NRRL B-12074 for making heteropolysaccharide
EP0598009B1 (fr) Production continue de natamycine
US5902579A (en) Natamycin-containing streptomyces biomass and its use in animal feed
EP0136805B1 (fr) Procédé de production de polyols par fermentation de sucres à l'échelle industrielle
CN1170761A (zh) 生产脂抑制素和四氢脂抑制素的方法
EP1613759B1 (fr) Procedes de fermentation presentant de faibles concentrations en nutriments contenant du carbone ou de l'azote
El-Enshasy et al. Improvement of rifemycins production by Amycolatopsis mediterranei in batch and fed-batch cultures
SU539538A3 (ru) Способ получени метаболита "а 27 106
CA1292713C (fr) Procede de production d'un antibiotique, la salinomycine
CA1297057C (fr) Methode de production de la ribavirine au moyen de sources de ribose tres concetree
EP0044659A2 (fr) Procédé pour la préparation de gomme de xanthane en utilisant le Xanthomonas Campestris ATCC 31.601
Málek et al. Continuous cultivation of microorganisms: A review
Humphrey et al. Fermentation. Unit Processes Review
KR910000464B1 (ko) 고농도배양에 의한 단세포단백질의 제조방법
US3043750A (en) Process for producing vitamins in the b group by means of propionic acid bacteria
Malek et al. Continuous cultivation of microorganisms
CN116426400A (zh) 一种多功能性微生物菌剂发酵生产工艺及系统
US2789941A (en) Process for producing bacitracin
Newaskar Regulation of antibiotic biosynthesis in continuous cultures of Penicillium urticae in a modified cyclone bioreactor
Efremenko Lactic acid production by immobilized fungus cells Rhizopus oryzae scaled up to the complex experimental system O. Spiricheva, O. Senko, I. Lyagin, V. Lozinsky 2, S. Varfolomeyev
NO774054L (no) Fremgangsmaate til fremstilling av encelleprotein

Legal Events

Date Code Title Description
AK Designated states

Kind code of ref document: A1

Designated state(s): AU BB BG BR CA CS FI HU JP KP KR LK MG MN MW NO PL RO RU SD

AL Designated countries for regional patents

Kind code of ref document: A1

Designated state(s): AT BE CH DE DK ES FR GB GR IE IT LU MC NL SE BF BJ CF CG CI CM GA GN ML MR SN TD TG

DFPE Request for preliminary examination filed prior to expiration of 19th month from priority date (pct application filed before 20040101)
WWE Wipo information: entry into national phase

Ref document number: 1992917836

Country of ref document: EP

WWE Wipo information: entry into national phase

Ref document number: 2115038

Country of ref document: CA

WWP Wipo information: published in national office

Ref document number: 1992917836

Country of ref document: EP

WWG Wipo information: grant in national office

Ref document number: 1992917836

Country of ref document: EP

DPE2 Request for preliminary examination filed before expiration of 19th month from priority date (pct application filed from 20040101)